EP2545977A1 - Wärmeintegration für die kryogene CO2-Trennung - Google Patents

Wärmeintegration für die kryogene CO2-Trennung Download PDF

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Publication number
EP2545977A1
EP2545977A1 EP20110173476 EP11173476A EP2545977A1 EP 2545977 A1 EP2545977 A1 EP 2545977A1 EP 20110173476 EP20110173476 EP 20110173476 EP 11173476 A EP11173476 A EP 11173476A EP 2545977 A1 EP2545977 A1 EP 2545977A1
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EP
European Patent Office
Prior art keywords
flue gas
refrigerant
heat exchanger
depleted
condenser
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP20110173476
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English (en)
French (fr)
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EP2545977B1 (de
Inventor
Olaf Stallman
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General Electric Technology GmbH
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Alstom Technology AG
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Filing date
Publication date
Priority to EP11173476.0A priority Critical patent/EP2545977B1/de
Application filed by Alstom Technology AG filed Critical Alstom Technology AG
Priority to ES11173476.0T priority patent/ES2582829T3/es
Priority to AU2012282201A priority patent/AU2012282201B2/en
Priority to CN201280034455.4A priority patent/CN103687659A/zh
Priority to CA2841219A priority patent/CA2841219A1/en
Priority to PCT/IB2012/001312 priority patent/WO2013008067A1/en
Publication of EP2545977A1 publication Critical patent/EP2545977A1/de
Priority to US14/152,251 priority patent/US20140123700A1/en
Application granted granted Critical
Publication of EP2545977B1 publication Critical patent/EP2545977B1/de
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/50—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2900/00—Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
    • F23J2900/15061—Deep cooling or freezing of flue gas rich of CO2 to deliver CO2-free emissions, or to deliver liquid CO2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/70—Flue or combustion exhaust gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
    • F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/30—Technologies for a more efficient combustion or heat usage
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/32—Direct CO2 mitigation

Definitions

  • the present invention relates to a method and a system for separating CO 2 from a CO 2 rich flue gas stream by refrigeration of the flue gas stream to condense CO 2 present therein.
  • a hot process gas is generated, such process gas containing, among other components, carbon dioxide CO 2 .
  • process gas containing, among other components, carbon dioxide CO 2 .
  • CO 2 capture often comprises cooling, or compression and cooling, of the flue gas to condense CO 2 in liquid or solid form and separate it from non-condensable flue gas components, such as N 2 and O 2 .
  • gas cleaning operation may generally include removal of dust, sulfur compounds, metals, nitrogen oxides, etc.
  • Cooling of the flue gas to its condensation temperature may be achieved by various means, e.g. using a suitable external refrigerant.
  • CO 2 capture systems using an external refrigerant can be expensive, both in terms of investment costs and in terms of operational costs.
  • auto-refrigeration systems are often used, wherein the CO 2 rich flue gas is compressed, cooled and expanded to achieve condensation of the CO 2 .
  • An object of the present invention is to provide a system and a method for removal of carbon dioxide from a flue gas stream, e.g. generated in a boiler combusting a fuel in the presence of a gas containing oxygen, the system and method alleviating at least one of the above mentioned problems.
  • the flue gas treatment systems and methods for removal of CO 2 from the flue gas stream according to various aspects described herein allow for cost effective separation of CO 2 using simple and robust heat exchanger designs and materials.
  • a refrigeration system for condensation of carbon dioxide (CO 2 ) in a flue gas stream comprising a flue gas compressor, at least one flue gas adsorption drier, a refrigeration system for condensation of carbon dioxide (CO 2 ), in a flue gas stream, said system comprising a refrigeration circuit containing a refrigerant, said refrigeration circuit comprising; a multistage refrigerant compressor, a refrigerant condenser, a refrigerant chiller, a flue gas chiller, at least one condenser, and a stripper column allowing distillation; wherein the flue gas chiller is arranged between the flue gas compressor and the flue gas adsorption drier and the the flue gas adsorption drier and the at least one condenser are arranged in series upstream of the stripper column.
  • the flue gas treatment system further comprises a another condenser, the first condenser, being arranged in memorized for the first condenser.
  • the efficiency of energy consumption may be optimised as the cooling may be performed step-wise, instead of in only one step.
  • the flue gas treatment system further comprising a heat exchanger configured to cool at least a portion of the condensed refrigerant using the CO 2 depleted flue gas from the second CO 2 condenser.
  • the flue gas treatment system further comprises a first heat exchanger configured to cool at least a portion of the condensed refrigerant using the CO2 depleted flue gas from the stripper column, a second heat exchanger configured to reheat the CO 2 depleted flue gas from the first refrigerant chiller using warm flue gas from the flue gas compressor, a first flue gas expander configured to expand the reheated compressed CO 2 depleted flue gas from the first heat exchanger, a third heat exchanger configured to further cool the condensed refrigerant from the first refrigerant chiller using the using the CO 2 depleted flue gas from the flue gas expander, a fourth heat exchanger configured to reheat the CO 2 depleted flue gas from the second heat exchanger using warm flue gas from the flue gas compressor, a second flue gas expander configured to expand the reheated compressed CO 2 depleted flue gas from the second heat exchanger, and optionally, a fifth heat exchanger configured to reheat
  • the flue gas treatment system further comprises a first heat exchanger configured to cool at least a portion of the condensed refrigerant using the CO 2 depleted flue gas from the stripper column, a second heat exchanger configured to reheat the CO 2 depleted flue gas from the first heat exchanger using warm flue gas from the flue gas compressor, a first flue gas expander configured to expand the reheated compressed CO 2 depleted flue gas from the second heat exchanger, a third heat exchanger configured to further cool the condensed refrigerant from the first heat exchanger using the using the CO 2 depleted flue gas from the flue gas expander, a second flue gas expander configured to expand the reheated compressed CO 2 depleted flue gas from the second heat exchanger, and a fourth heat exchanger configured to reheat the CO 2 depleted flue gas from the third exchanger.
  • a first heat exchanger configured to cool at least a portion of the condensed refrigerant using the CO 2 depleted flue gas from
  • the flue gas treatment system further comprises a selective catalytic reduction (SCR) unit for removal of nitrogen oxides (NOx) from the flue gas stream, arranged downstream of the flue gas adsorption drier, with reference to the general flow direction of the CO 2 depleted flue gas stream.
  • SCR selective catalytic reduction
  • a method for condensation of carbon dioxide (CO 2 ) in a flue gas stream using a circulating stream of an external refrigerant comprising
  • the said external refrigerant is propane or propylene.
  • the said external refrigerant is ammonia.
  • Pressures herein are in the unit "bar”, and denote absolute pressures unless indicated otherwise.
  • indirect or “indirectly” as used herein in connection with heat exchange between two fluids, such as heating, cooling or chilling, denotes that the heat exchange occurs without mixing the two fluids together.
  • indirect heat exchange may for example be performed in an indirect-contact heat exchanger, wherein the fluid streams remain separate and the heat transfers continuously through an impervious dividing wall.
  • the refrigeration system or flue gas treatment system of the various aspects disclosed herein may for example be implemented in a combustion plant, such as a fossil fired boiler system.
  • a combustion plant such as a fossil fired boiler system.
  • the applications of the system and method is not limited, typically they are useful for all gas streams having an increased CO2 concentration, for example CO2 concentration of above 50 %.
  • the flue gas leaving a fossil fired oxy boiler system will contain 50-80 % by volume of carbon dioxide.
  • the balance of the "carbon dioxide rich flue gas” will be about 15-40% by volume of water vapour (H 2 O), 2-7 % by volume of oxygen (O 2 ),since a slight oxygen excess is often preferred in the boiler, and totally about 0-10 % by volume of other gases, including mainly nitrogen (N 2 ) and argon (Ar), since some leakage of air can seldom be completely avoided.
  • the carbon dioxide rich flue gas generated in a fossil fired oxy boiler system may typically comprise contaminants in the form of, for example, dust particles, hydrochloric acid, HCl, nitrous oxides, NO x , sulfur oxides, SO x , and heavy metals, including mercury, Hg.
  • CO 2 separation in the embodiments described herein is achieved by means of compression of the flue gas and condensation by refrigeration.
  • Fig. 1 schematically illustrates a CO 2 separation system for condensation of carbon dioxide (CO 2 ) in a flue gas stream.
  • the CO 2 separation system of Fig. 1 may be implemented in any fossil fired oxy boiler system.
  • the CO 2 separation system 10 comprises a flue gas conduit 55 operative for forwarding flue gas from a boiler to a stack, optionally via one or more flue gas treatment units, such as a dust removal device, a sulfur dioxide removal system, and a flue gas condenser.
  • the CO 2 separation system 10 may optionally comprise at least one compressor 44 having at least one, and typically two to ten compression stages for compressing the carbon dioxide rich flue gas.
  • the flue gas compressor is operative for compressing the flue gas to a pressure at which gaseous CO 2 is converted to liquid form when the temperature of the flue gas is reduced in at least one CO 2 condenser 70, for example in two CO 2 condensers 64, 70.
  • the carbon dioxide rich flue gas is generally compressed to a pressure of about 20 bar or higher, such as about 33 bar, in the multistage compressor.
  • Each compression stage could be arranged as a separate unit.
  • several compression stages could be operated by a common drive shaft.
  • the compressor 44 may also comprise an intercooling unit (not shown), downstream of one or more of the compression stages. The intercooling unit may further be configured to collect and dispose of any liquid condensate formed during compression and/or cooling of the carbon dioxide rich flue gas.
  • the CO 2 separation system 10 comprises a refrigeration system 50 having a refrigeration circuit 51 containing refrigerant in liquid and/or vapor form.
  • refrigerants can be used to supply the cooling and condensing duties required for condensation of CO 2 in the refrigeration system.
  • refrigerants examples include propane (R290) and propylene (R1270) and mixtures thereof. Another option is ammonia. Also other refrigerants having the desired thermodynamic and chemical properties can also be used as desired.
  • the refrigeration circuit 51 comprises a multistage refrigerant 52 compressor configured to compress the refrigerant to a predetermined pressure.
  • the multistage compressor 52 may for example have three or more compression stages, each compression stage configured to compress the refrigerant to a certain pressure level.
  • the multistage compressor 52 may be provided with intercooling between two or more of the compression stages.
  • Cold, gaseous refrigerant is compressed from a low pressure within the multistage compressor 52 to a pressure P0, for example in the range of about 8 to 25 bar (depending on the refrigerant and condensing medium temperature), and directed into refrigerant condenser 53.
  • High pressure refrigerant is then substantially condensed within refrigerant condenser 53, which may be cooled by water, forced air or the like.
  • the condensed refrigerant is distributed to a flue gas chiller 60, a first CO 2 condenser 64 and a second CO 2 condenser 70, where it is used for chilling the flue gas containing CO 2 .
  • the flue gas chiller 60 comprises a metering device, for example an expansion valve (not shown), for reducing the pressure and inducing evaporation of the condensed refrigerant.
  • the flue gas chiller further comprises a heat exchanger, in which the refrigerant is expanded to a pressure P1, for example about 5 bar, and the boiling refrigerant is used to indirectly chill the flue gas stream to a temperature in the range of about 10-20 °C. Water which precipitates from the flue gas during the chilling in the flue gas chiller is separated from the flue gas stream and removed via line 61.
  • the chilled flue gas depleted in water vapor from the flue gas chiller is then forwarded to the first CO 2 condenser 64, optionally via an adsorption drier (not shown).
  • the first CO 2 condenser 64 comprises a metering device, for example an expansion valve (not shown), for reducing the pressure and inducing evaporation of the condensed refrigerant.
  • the first CO 2 condenser 64 further comprises a heat exchanger, in which liquefied refrigerant is expanded to a pressure P2 ( ⁇ P1), for example about 2.7 bar, and the boiling refrigerant is used to indirectly chill the flue gas stream to a temperature of about -20 °C, causing at least a portion of the CO 2 from the flue gas to condense.
  • the first CO 2 condenser 64 further comprises a first gas/liquid separator 65.
  • the gas/liquid separator 65 separates condensed CO 2 in liquid form from the residual partially CO 2 depleted flue gas (vent gas).
  • the liquefied CO 2 leaves the gas/liquid separator 65 via line 66 and is pumped to a CO 2 product drum by CO 2 product pump 67.
  • the vent gas leaves the gas/liquid separator 65 via line 68.
  • the partially CO 2 depleted ventgas is forwarded via line 68 to the second CO 2 condenser 70.
  • the second CO 2 condenser 70 comprises a metering device, for example an expansion valve (not shown), for reducing the pressure and inducing evaporation of the condensed refrigerant.
  • the second CO 2 condenser 70 further comprises a heat exchanger, in which liquefied refrigerant is expanded to a pressure P3 ( ⁇ P2), for example atmospheric pressure (about 1 bar), and the boiling refrigerant is used to indirectly chill the flue gas stream to a temperature of about -42 °C, causing at least a portion of the CO 2 from the flue gas to condense.
  • the refrigeration temperature is limited by the minimal achievable temperature of the refrigerant. For propylene or propane, this temperature limit would be about - 45 °C at ambient pressure level.
  • the partially condensed flue gas stream from the second CO 2 condenser 70 is forwarded to a stripper column 71 for distillative purification of the liquid.
  • the stream is fed to the column at the top and the liquid portion serves as the required reflux.
  • the stripper column does not require any overhead condensation system for reflux generation. Consequently, the overall investment cost of the system is minimised.
  • the liquefied CO 2 runs down the stripper column and is intensively contacted with the upflowing gas. This contacting is extracting (stripping) trace impurities of the liquid CO2 and thus the concentration of the CO2 is increased.
  • the purified CO2 leaves the stripper column 71 via line 72 to a stripper reboiler 84. In the reboiler a part of the CO2 is vaporized to generate the required gas stream for the column. The heat is provided by subcooling a part of the refrigerant.
  • the remaining liquid may be extracted either from the column sump or, as shown, from the reboiler and subsequently, is pumped to a CO 2 product drum by CO 2 pump 86, via another heat exchanger 85 where the refrigerant is cooled to about 1-5 °C, for example 3-4 °C. From the drum the CO2 product is raised in pressure by CO 2 product pump 88 to the level required for further processing.
  • the refrigeration system 50 further comprises a refrigerant chiller 80.
  • the refrigerant chiller 80 comprises a heat exchanger configured to chill refrigerant by indirect contact with cold purified liquid CO 2 from the stripper column 71.
  • the temperature of the condensed CO 2 from the first and second CO 2 condensers 64, 70 may generally be about -20 °C and -42 °C respectively.
  • the temperature of the refrigerant may be reduced from in the range of about 15-30 °C to about 1 °C in the refrigerant chiller 80.
  • Evaporated refrigerant from the flue gas chiller 60, the first CO 2 condenser 64 and the second CO 2 condenser 70 is returned to the multistage compressor 52 for recompression and, after condensation, use for further cooling of the flue gas stream.
  • the evaporated refrigerant from the the flue gas chiller 60 at a pressure P1, for example about 5 bar, is forwarded to a first compression stage 52' of the multistage compressor 52 suitable for receiving refrigerant at a pressure of P1.
  • the evaporated refrigerant streams are then recompressed to pressure P0 and reused in the refrigeration circuit.
  • the liquid CO 2 product from the refrigerant chiller 80 may be collected in a CO 2 product drum 87 and can then be pumped by CO 2 product pump 88 to a pressure level suitable for transportation or further processing. If the pressure would be increased to this level in a single step in CO 2 product pump 67 or 73, the pump would introduce too much heat into the CO 2 product stream and thereby reduce the duty available for chilling of the refrigerant in the refrigerant chiller and/or auxiliary refrigerant chiller(s).
  • Fig. 2 schematically depicts an embodiment of a CO 2 separation system integrated into a flue gas treatment system for removing CO 2 from a flue gas stream, for example a flue gas stream generated in a boiler combusting a fuel in the presence of a gas containing oxygen.
  • the CO 2 separation system 110 comprises at least one compressor 144 having at least one, and typically two to ten compression stages for compressing the carbon dioxide rich flue gas.
  • the flue gas compressor 144 is operative for compressing the flue gas to a pressure at which gaseous CO 2 is converted to liquid form when the temperature of the flue gas is reduced in the CO 2 condensers 164, 170.
  • the carbon dioxide rich flue gas is generally compressed to a pressure of about 20 bar or higher, such as about 33 bar, in the multistage compressor.
  • Each compression stage could be arranged as a separate unit. As an alternative several compression stages could be operated by a common drive shaft.
  • the compressor 144 may also comprise an intercooling unit (not shown), downstream of one or more of the compression stages. The intercooling unit may further be configured to collect and dispose of any liquid condensate formed during compression and/or cooling of the carbon dioxide rich flue gas.
  • the CO 2 separation system 110 may further comprise an adsorption drier 162 operative for removing at least a portion of the remaining water vapor in the CO 2 rich flue gas stream.
  • the adsorption drier 162 is provided with a packing comprising a water vapor adsorbent, also referred to as a desiccant, having affinity for water vapour.
  • the desiccant may, for example, be silica gel, calcium sulfate, calcium chloride, montmorillonite clay, molecular sieves, or another material that is, as such, known for its use as a desiccant.
  • the drier material may preferably be selected such that it can withstand eventually forming acids. This allows omitting additional steps for removal of SO x and NO x compounds that could otherwise harm the integrity of the adsorbent.
  • the adsorption drier 162 may be provided with a regeneration and heating system for intermittent regeneration of the water vapour adsorption capacity of the adsorption drier.
  • a supply duct 190 is arranged for supplying a regeneration gas to the system.
  • the regeneration gas is preferably an inert gas which does not react with the packing of the adsorption drier. Examples of suitable gases include nitrogen or another inert gas that, preferably, holds a low amount of mercury and water vapour.
  • vent gas usually comprising nitrogen as one of its main constituents, separated from the carbon dioxide in the CO 2 separation system 110 is utilized as regeneration gas.
  • the regeneration system comprises a heater 191 which is adapted for heating the regeneration gas.
  • a heating circuit is connected to the heater for circulating a heating medium, such as steam, in the heater.
  • a heating medium such as steam
  • the heater may typically heat the regeneration gas to a temperature of about 120-300 °C.
  • the heated regeneration gas is supplied to the adsorption drier 162 from the regeneration and heating system. The regeneration gas heats the material of the packing and causes desorption of water vapour.
  • the system may be provided with two parallel adsorption driers, with one of those parallel adsorption driers being in operation while the other parallel adsorption drier undergoes regeneration.
  • the carbon dioxide rich flue gas could be emitted to the atmosphere during the regeneration of the packing of the adsorption drier.
  • the flue CO 2 separation system 110 comprises a refrigeration system 150 for condensation of carbon dioxide in the flue gas stream.
  • the refrigeration system 150 comprises a refrigeration circuit 151 containing refrigerant in liquid and/or vapor form.
  • refrigerants can be used to supply the cooling and condensing duties required for condensation of CO 2 in the refrigeration system. Examples of refrigerants that can be used include propane (R290) and propylene (R1270) and mixtures thereof. Other refrigerants having the desired thermodynamic and chemical properties also can be used as desired.
  • the refrigeration circuit 151 comprises a multistage refrigerant compressor 152 configured to compress the refrigerant to a predetermined pressure.
  • the multistage compressor may for example have three or more compression stages, each compression stage configured to compress the refrigerant to a certain pressure level.
  • the multistage compressor may be provided with intercooling between two or more of the compression stages.
  • gaseous refrigerant is compressed from a low pressure within the multistage compressor 152 to a pressure P0, for example in the range of about 8 to about 25 bar (depending on the refrigerant and condensing medium temperature), and directed into refrigerant condenser 153.
  • High pressure refrigerant is then substantially condensed within refrigerant condenser 153, which may be cooled by water, forced air or the like.
  • the condensed refrigerant is distributed to a flue gas chiller 160, a first CO 2 condenser 164 and a second CO 2 condenser 170, where it is used for chilling the flue gas containing CO 2 travelling in the flue gas conduit 155.
  • the flue gas chiller 160 comprises a metering device, for example an expansion valve (not shown), for reducing the pressure and inducing evaporation of the condensed refrigerant.
  • the flue gas chiller further comprises a heat exchanger, in which the refrigerant is expanded to a pressure P1, for example about 5 bar, and the boiling refrigerant is used to indirectly chill the flue gas stream to a temperature in the range of about 6 to 20 °C. Water which precipitates from the flue gas during the chilling in the flue gas chiller is separated from the flue gas stream and removed via line 161. The chilled flue gas depleted in water vapor from the flue gas chiller is then forwarded to the adsorption drier 162.
  • the chilled and dried flue gas from the adsorption drier 162 is forwarded to the first CO 2 condenser 164.
  • the first CO 2 condenser comprises a metering device, for example an expansion valve (not shown), for reducing the pressure and inducing evaporation of the condensed refrigerant.
  • the first CO 2 condenser further comprises a heat exchanger, in which liquefied refrigerant is expanded to a pressure P2 ( ⁇ P1), for example about 2.7 bar, and the boiling refrigerant is used to indirectly chill the flue gas stream to a temperature of about -20 °C, causing at least a portion of the CO 2 from the flue gas to condense.
  • the first CO 2 condenser 164 further comprises a first gas/liquid separator 165.
  • the gas/liquid separator 165 separates condensed CO 2 in liquid form from the residual partially CO 2 depleted flue gas (vent gas).
  • the liquefied CO 2 leaves the gas/liquid separator 165 via line 166 and is forwarded to the stripper column 171.
  • the partially CO 2 depleted ventgas is forwarded via line 168 to the second CO 2 condenser 170.
  • the second CO 2 condenser 170 comprises a metering device, for example an expansion valve (not shown), for reducing the pressure and inducing evaporation of the condensed refrigerant.
  • the second CO 2 condenser further comprises a heat exchanger, in which liquefied refrigerant is expanded to a pressure P3 ( ⁇ P2), for example atmospheric pressure (about 1 bar), and the boiling refrigerant is used to indirectly chill the flue gas stream to a temperature of about -42 °C, causing at least a portion of the CO 2 from the flue gas to condense.
  • the refrigeration temperature is limited by the minimal achievable temperature of the refrigerant. For propylene or propane, this temperature limit would be about - 45 °C at ambient pressure level.
  • the partially condensed flue gas stream from the second CO 2 condenser 170 is forwarded to a stripper column 171 for distillative purification of the liquid.
  • the stream is fed to the column at the top and the liquid portion serves as the required reflux.
  • the stripper column does not require any overhead condensation system for reflux generation. Consequently, the overall investment cost of the system is minimised.
  • the liquefied CO 2 runs down the stripper column and is intensively contacted with the upflowing gas. This contacting is extracting (stripping) trace impurities of the liquid CO2 and thus the concentration of the CO2 is increased.
  • the purified CO2 leaves the stripper column 171 via line 172 to a stripper reboiler 184.
  • a part of the CO2 is vaporized to generate the required gas stream for the column.
  • the heat is provided by subcooling a part of the refrigerant.
  • the remaining liquid may be extracted either from the column sump or, as shown, from the reboiler and subsequently, is pumped to a CO 2 product drum by CO 2 pump 186, via another heat exchanger 185 where the refrigerant is cooled to about 1-5 °C, for example 3-4 °C. From the drum the CO2 product is raised in pressure by CO 2 product pump 188 to the level required for further processing.
  • the refrigeration system 150 further comprises a refrigerant chiller 180.
  • the refrigerant chiller 180 comprises a heat exchanger configured to chill refrigerant by indirect contact with cold purified liquid CO 2 from the stripper column 171.
  • the temperature of the condensed CO 2 from the first and second CO 2 condensers 164, 170 may generally be about -20 °C and -42 °C respectively.
  • the temperature of the refrigerant may be reduced from in the range of about 15-30 °C to about 1 °C in the refrigerant chiller 180.
  • the refrigeration system 150 further comprises a refrigerant chiller 180.
  • the refrigerant chiller 180 comprises a heat exchanger configured to chill refrigerant by indirect contact with cold purified liquid CO 2 from the stripper column.
  • the temperature of the condensed CO 2 from the first and second CO 2 condensers 164, 170 may generally be about -20 °C and -42 °C respectively.
  • the temperature of the refrigerant may be reduced from in the range of about 15-30 °C to about 1 °C in the refrigerant chiller 180.
  • the chilled refrigerant from the refrigerant chiller 180 is split and distributed via lines 181, 182, 183 to the flue gas chiller 160, first CO 2 condenser 164 and second CO 2 condenser 170.
  • the quantity of refrigerant distributed to each of the flue gas chiller 160, the first CO 2 condenser 164 and the second CO 2 condenser 170 may be selected so as to provide the desired refrigeration in each heat exchanger.
  • the liquid CO 2 product from the refrigerant chiller 180 may be collected in a CO 2 product drum 187 and can then be pumped by CO 2 product pump 188 to a pressure level suitable for transportation or further processing. If the pressure would be increased to this level in a single step in CO 2 product pump 167 or 173, the pump would introduce too much heat into the CO 2 product stream and thereby reduce the duty available for chilling of the refrigerant in the refrigerant chiller and/or auxiliary refrigerant chiller(s).
  • the refrigeration system 150 in Fig. 2 further comprises an arrangement for precooling at least a portion of the condensed refrigerant coming from the refrigerant condenser using the cold CO 2 depleted flue gas from the second CO 2 condenser.
  • the arrangement comprises a first heat exchanger 192 configured for cooling the refrigerant coming from the refrigerant condenser 153, by indirect contact with cold CO 2 depleted flue gas from the second CO 2 condenser 170 via line 174.
  • a second heat exchanger 193 is configured to reheat the CO 2 depleted flue gas from the first heat exchanger 192 using warm flue gas from the flue gas compressor 144.
  • a flue gas expander 194 is configured to expand the reheated compressed CO 2 depleted flue gas from the second heat exchanger resulting in a reduction of temperature of the flue gas.
  • the flue gas from the flue gas expander 194 is forwarded to a third heat exchanger 195 where it is used to further cool the condensed refrigerant from the first heat exchanger.
  • the arrangement further comprises a fourth heat exchanger 196 configured to reheat the CO 2 depleted flue gas from the third heat exchanger 195 using warm flue gas from the flue gas compressor 144, a second flue gas expander 197 configured to expand the reheated CO 2 depleted flue gas from the fourth heat exchanger 196 resulting in a reduction of temperature of the flue gas, and a fifth heat exchanger 198 configured to reheat the expanded flue gas from the second flue gas expander 197 using warm flue gas from the flue gas compressor 144.
  • a fourth heat exchanger 196 configured to reheat the CO 2 depleted flue gas from the third heat exchanger 195 using warm flue gas from the flue gas compressor 144
  • a second flue gas expander 197 configured to expand the reheated CO 2 depleted flue gas from the fourth heat exchanger 196 resulting in a reduction of temperature of the flue gas
  • a fifth heat exchanger 198 configured to reheat the expanded flue gas from the second flue
  • This optional arrangement provides a reheated flue gas which is suitable, possibly after additional heating in a regeneration gas heater 191, for use as a regeneration gas for regeneration of the adsorption drier 162 as described above.
  • the reheated flue gas may be forwarded to an (optional) SCR unit for removal of nitrogen oxides from the flue gas by selective catalytic reduction to N 2 .
  • Evaporated refrigerant from the flue gas chiller160, the first CO 2 condenser 164 and the second CO 2 condenser 170 is returned to the multistage compressor 152 for recompression and use for further cooling of the flue gas stream.
  • the evaporated refrigerant from the the flue gas chiller 160 at a pressure P1, for example about 5 bar, is forwarded to a first compression stage 152' of the multistage compressor 152 suitable for receiving refrigerant at a pressure of P1.
  • the evaporated refrigerant streams are then recompressed to pressure P0 and reused in the refrigeration circuit.
  • the CO 2 separation system 210 comprises a refrigeration system 250.
  • the refrigeration system 250 comprises a refrigeration circuit 251 containing refrigerant in liquid and/or vapor form.
  • refrigerants can be used to supply the cooling and condensing duties required for condensation of CO 2 in the refrigeration system. Examples of refrigerants that can be used include R290 (propane) and R1270 propylene and mixtures thereof. Another option of refrigerants is ammonia. Other refrigerants having the desired thermodynamic and chemical properties also can be used as desired.
  • the refrigeration circuit comprises a multistage refrigerant compressor 252 configured to compress the refrigerant to a predetermined pressure.
  • the multistage compressor may for example have three or more compression stages, each compression stage configured to compress the refrigerant to a certain pressure level.
  • the multistage compressor may be provided with intercooling between two or more of the compression stages.
  • gaseous refrigerant is compressed from a low pressure within the multistage compressor 252 to a pressure P0, for example in the range of about 8 to about 25 bar (depending on the refrigerant and condensing medium temperature), and directed into refrigerant condenser 253.
  • Pressure P0 for example in the range of about 8 to about 25 bar (depending on the refrigerant and condensing medium temperature)
  • High pressure refrigerant is then substantially condensed within refrigerant condenser 253, which may be cooled by water, forced air or the like.
  • the refrigeration circuit 251 comprises a liquid split which splits the refrigerant flow from the refrigerant condenser 253 into a first and second portion.
  • the first portion of the condensed refrigerant is directed via line 254a to a refrigerant chiller 280 configured to chill the portion of the condensed refrigerant using liquid CO 2 separated in the stripper column 271.
  • the second portion of the condensed refrigerant is directed via line 254b to a heat exchanger arrangement configured to cool a second portion of the condensed refrigerant using the CO 2 depleted flue gas from the second CO 2 condenser 270.
  • the first portion of the condensed refrigerant is forwarded from the refrigerant condenser 253 to the refrigerant chiller 280 via line 254a.
  • the refrigerant chiller comprises a heat exchanger configured to chill refrigerant by indirect contact with cold condensed CO 2 from the stripper column 271.
  • the partially condensed flue gas stream from the second CO 2 condenser 270 is forwarded to a stripper column 271 for distillative purification of the liquid.
  • the stream is fed to the column at the top and the liquid portion serves as the required reflux.
  • the stripper column does not require any overhead condensation system for reflux generation. Consequently, the overall investment cost of the system is minimised.
  • the liquefied CO 2 runs down the stripper column and is intensively contacted with the upflowing gas. This contacting is extracting (stripping) trace impurities of the liquid CO 2 and thus the concentration of the CO 2 is increased.
  • the purified CO 2 leaves the stripper column 271 via line 272 to a stripper reboiler 284. In the reboiler a part of the CO 2 is vaporized to generate the required gas stream for the column. The heat is provided by subcooling the required gas stream for the column.
  • the heat is provided by subcooling a part of the refrigerant.
  • the remaining liquid may be extracted either from the column sump or, as shown, from the reboiler and subsequently, is pumped to a CO 2 product drum by CO 2 pump 81, via another heat exchanger 285 where the refrigerant is cooled to about 1-5 °C, for example 3-4 °C.
  • CO 2 pump 81 the refrigerant is cooled to about 1-5 °C, for example 3-4 °C.
  • From the drum the CO2 product is raised in pressure by CO 2 product pump 288 to the level required for further processing.
  • the refrigeration system 250 further comprises a refrigerant chiller 280.
  • the refrigerant chiller 280 comprises a heat exchanger configured to chill refrigerant by indirect contact with cold purified liquid CO 2 from the stripper column 71.
  • the temperature of the condensed CO 2 from the first and second CO 2 condensers 264, 270 may generally be about -20 °C and -42 °C respectively.
  • the temperature of the refrigerant may be reduced from in the range of about 15-30 °C to about 1 °C in the refrigerant chiller 280.
  • the quantity of refrigerant distributed to each of the flue gas chiller 260, the first CO 2 condenser 264 and the second CO 2 condenser 270 may be selected so as to provide the desired refrigeration in each heat exchanger.
  • the flue gas chiller 260 comprises a metering device, for example an expansion valve (not shown), for reducing the pressure and inducing evaporation of the condensed refrigerant.
  • the flue gas chiller further comprises a heat exchanger, in which the refrigerant is expanded to a pressure P1, for example about 5 bar, and the boiling refrigerant is used to indirectly chill the flue gas stream to a temperature in the range of about 6 to 20 °C. Water which precipitates from the flue gas during the chilling in the flue gas chiller is separated from the flue gas stream and removed via line 261.
  • the chilled flue gas depleted in water vapor from the flue gas chiller is then forwarded to the first CO 2 condenser 264, optionally via an adsorption drier 262.
  • the first CO 2 condenser comprises a metering device, for example an expansion valve (not shown), for reducing the pressure and inducing evaporation of the condensed refrigerant.
  • the first CO 2 condenser further comprises a heat exchanger, in which liquefied refrigerant is expanded to a pressure P2 ( ⁇ P1), for example about 2.7 bar, and the boiling refrigerant is used to indirectly chill the flue gas stream to a temperature of about -20 °C, causing at least a portion of the CO 2 from the flue gas to condense.
  • the first CO 2 condenser 264 further comprises a first gas/liquid separator 265.
  • the gas/liquid separator 265 separates condensed CO 2 in liquid form from the residual partially CO 2 depleted flue gas (vent gas).
  • the liquefied CO 2 leaves the first gas/liquid separator 265 via line 266 and is pumped by CO 2 product pump 267 to a pressure, for example about 60 bar, sufficient to prevent evaporation of the CO 2 product when it is used for cooling the refrigerant in the refrigerant chiller 280.
  • the vent gas leaves the gas/liquid separator 265 via line 268.
  • the partially CO 2 depleted ventgas is forwarded via line 268 to the second CO 2 condenser 270.
  • the second CO 2 condenser comprises a metering device, for example an expansion valve (not shown), for reducing the pressure and inducing evaporation of the condensed refrigerant.
  • the second CO 2 condenser further comprises a heat exchanger, in which liquefied refrigerant is expanded to a pressure P3 ( ⁇ P2), for example atmospheric pressure (about 1 bar), and the boiling refrigerant is used to indirectly chill the flue gas stream to a temperature of about -42 °C, causing at least a portion of the CO 2 from the flue gas to condense.
  • the refrigeration temperature is limited by the minimal achievable temperature of the refrigerant.
  • the second CO 2 condenser further comprises a gas/liquid separator 271.
  • the gas/liquid separator 271 separates condensed CO 2 in liquid form from the residual partially CO 2 depleted flue gas (vent gas).
  • the partially condensed flue gas stream from the second CO 2 condenser 270 is forwarded to a stripper column 271 for distillative purification of the liquid.
  • the stream is fed to the column at the top and the liquid portion serves as the required reflux.
  • the stripper column does not require any overhead condensation system for reflux generation. Consequently, the overall investment cost of the system is minimised.
  • the liquefied CO 2 runs down the stripper column and is intensively contacted with the upflowing gas. This contacting is extracting (stripping) trace impurities of the liquid CO 2 and thus the concentration of the CO2 is increased.
  • the purified CO 2 leaves the stripper column 271 via line 272 to a stripper reboiler 284. In the reboiler a part of the CO 2 is vaporized to generate the required gas stream for the column. The heat is provided by subcooling a part of the refrigerant.
  • the remaining liquid may be extracted either from the column sump or, as shown, from the reboiler and subsequently, is pumped to a CO 2 product drum by CO 2 pump 286, via another heat exchanger where the refrigerant is cooled to about 1-5 °C, for example 3-4 °C. From the drum the CO2 product is raised in pressure by CO 2 product pump 288 to the level required for further processing.
  • the second portion of the condensed refrigerant is directed via line 254b to a heat exchanger arrangement configured to cool a second portion of the condensed refrigerant using the CO 2 depleted flue gas from the second CO 2 condenser 270.
  • the heat exchanger arrangement comprises two heat exchangers 292a, 292b arranged in parallel.
  • the second portion of the condensed refrigerant from the refrigerant condenser is divided into two substreams, each directed towards one of the two heat exchangers via lines 254b1 and 254b2 respectively.
  • the heat exchanger 292a is configured to cool substream 254b1 of the condensed refrigerant using the CO 2 depleted flue gas from the second CO 2 condenser 270.
  • the heat exchanger 293 is configured to reheat the CO 2 depleted flue gas from the heat exchanger 292a using the warm flue gas from the flue gas compressor 244.
  • a flue gas expander 294 is configured to expand the reheated compressed CO 2 depleted flue gas from the heat exchanger 293.
  • the heat exchanger 292b is configured to cool substream 254b2 of the condensed refrigerant using the CO 2 depleted flue gas from the flue gas expander 294.
  • the cooled first and second substreams from the heat exchangers 292a, 292b are combined and forwarded via line 295 to line 283, where it is combined with the refrigerant coming from the auxiliary refrigerant chiller 286.
  • the arrangement further comprises a heat exchanger 296 configured to reheat the CO 2 depleted flue gas from the heat exchanger 292b using warm flue gas from the flue gas compressor 244, a second flue gas expander 297 configured to expand the reheated CO 2 depleted flue gas from the heat exchanger 296 resulting in a reduction of temperature of the flue gas, and a heat exchanger 298 configured to reheat the expanded flue gas from the second flue gas expander 297 using warm flue gas from the flue gas compressor 244.
  • This optional arrangement provides a reheated flue gas which is suitable, possibly after additional heating in a regeneration gas heater 291, for use as a regeneration gas for regeneration of the adsorption drier 262 as described above.
  • the reheated flue gas may be forwarded to an (optional) SCR unit for removal of nitrogen oxides from the flue gas by selective catalytic reduction to N 2 .
  • Evaporated refrigerant from the flue gas chiller 260, the first CO 2 condenser 264 and the second CO 2 condenser 270 is returned to the multistage compressor 252 for recompression and use for further cooling of the flue gas stream.
  • the evaporated refrigerant from the the flue gas chiller 260 at a pressure P1, for example about 5 bar, is forwarded to a first compression stage 252' of the multistage compressor 252 suitable for receiving refrigerant at a pressure of P1.
  • the evaporated refrigerant streams are then recompressed in the multistage compressor 252 to pressure P0 and reused in the refrigeration circuit.

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EP11173476.0A 2011-07-11 2011-07-11 Wärmeintegration für die kryogene CO2-Trennung Active EP2545977B1 (de)

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ES11173476.0T ES2582829T3 (es) 2011-07-11 2011-07-11 Integración térmica para separación criogénica de CO2
EP11173476.0A EP2545977B1 (de) 2011-07-11 2011-07-11 Wärmeintegration für die kryogene CO2-Trennung
CN201280034455.4A CN103687659A (zh) 2011-07-11 2012-06-29 用于低温二氧化碳分离的热综合利用
CA2841219A CA2841219A1 (en) 2011-07-11 2012-06-29 Heat integration for cryogenic co2 separation
AU2012282201A AU2012282201B2 (en) 2011-07-11 2012-06-29 Heat integration for cryogenic CO2 separation
PCT/IB2012/001312 WO2013008067A1 (en) 2011-07-11 2012-06-29 Heat integration for cryogenic co2 separation
US14/152,251 US20140123700A1 (en) 2011-07-11 2014-01-10 Heat integration for cryogenic co2 separation

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CN110801639B (zh) * 2019-11-11 2021-06-01 杭州快凯高效节能新技术有限公司 一种工业尾气多级液化及分级制冷回收二氧化碳方法
EP4271952A1 (de) * 2020-12-30 2023-11-08 The Texas A&M University System Kryogene abscheidung von kohlendioxid, schwefeloxiden und stickoxiden aus rauchgas
FR3119227B1 (fr) * 2021-01-27 2023-03-10 Air Liquide Procédé et appareil de séparation d’un débit riche en dioxyde de carbone par distillation pour produire du dioxyde de carbone liquide

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CA2841219A1 (en) 2013-01-17
ES2582829T3 (es) 2016-09-15
EP2545977B1 (de) 2016-04-20
AU2012282201B2 (en) 2015-09-17
US20140123700A1 (en) 2014-05-08
CN103687659A (zh) 2014-03-26
WO2013008067A1 (en) 2013-01-17

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